WO2011104841A1 - Exhaust gas treatment system, and exhaust gas treatment method - Google Patents

Exhaust gas treatment system, and exhaust gas treatment method Download PDF

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WO2011104841A1
WO2011104841A1 PCT/JP2010/052956 JP2010052956W WO2011104841A1 WO 2011104841 A1 WO2011104841 A1 WO 2011104841A1 JP 2010052956 W JP2010052956 W JP 2010052956W WO 2011104841 A1 WO2011104841 A1 WO 2011104841A1
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exhaust gas
desulfurization
boiler
waste water
treatment
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Japanese (ja)
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鵜飼 展行
盛紀 村上
進 沖野
立人 長安
晴治 香川
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三菱重工業株式会社
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    • C02F9/00Multistage treatment of water, waste water, or sewage
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
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    • B01D53/34Chemical or biological purification of waste gases
    • B01D53/46Removing components of defined structure
    • B01D53/48Sulfur compounds
    • B01D53/50Sulfur oxides
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01D53/74General processes for purification of waste gases; Apparatus or devices specially adapted therefor
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    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D2251/00Reactants
    • B01D2251/40Alkaline earth metal or magnesium compounds
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    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D2257/00Components to be removed
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    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
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    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D2257/00Components to be removed
    • B01D2257/40Nitrogen compounds
    • B01D2257/404Nitrogen oxides other than dinitrogen oxide
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
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    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
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    • B01D2258/0283Flue gases
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1456Removing acid components
    • B01D53/1481Removing sulfur dioxide or sulfur trioxide
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D53/00Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34Chemical or biological purification of waste gases
    • B01D53/74General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86Catalytic processes
    • B01D53/8621Removing nitrogen compounds
    • B01D53/8625Nitrogen oxides
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    • C02F1/001Processes for the treatment of water whereby the filtration technique is of importance
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    • C02TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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    • C02F1/00Treatment of water, waste water, or sewage
    • C02F1/38Treatment of water, waste water, or sewage by centrifugal separation
    • C02F1/385Treatment of water, waste water, or sewage by centrifugal separation by centrifuging suspensions
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    • C02F1/44Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
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    • C02F1/00Treatment of water, waste water, or sewage
    • C02F1/46Treatment of water, waste water, or sewage by electrochemical methods
    • C02F1/469Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis
    • C02F1/4693Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis electrodialysis
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    • C02F1/52Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
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    • C02F1/68Treatment of water, waste water, or sewage by addition of specified substances, e.g. trace elements, for ameliorating potable water
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    • YGENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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Abstract

Disclosed is an exhaust gas treatment system (10A) which is provided with a boiler (11) for burning fuel, an air heater (13) for collecting the heat of the exhaust gas (17) from the boiler (11), and a desulfurization unit (15) which removes, by means of an absorption liquid, the sulfur oxide contained in the exhaust gas (17) after the heat thereof was collected, wherein a wastewater supplying means (P0 to P5), which supplies the desulfurization wastewater (28) that is discharged from the desulfurization unit (15), is disposed on at least one of the following locations: a path for supplying fuel to the boiler (11), inside the furnace of the boiler (11), or inside the smoke path between the boiler (11) and the air heater (13). As a consequence of having the abovementioned configuration, the amount of desulfurization wastewater, that is returned to the smoke path per unit time, can be increased compared to the prior art without having to increase the size of the entire exhaust gas treatment system.

Description

排ガス処理システム及び排ガス処理方法Exhaust gas treatment system and exhaust gas treatment method

 本発明は、ボイラから排出される排ガスを処理する排ガス処理システム及び方法に関する。 The present invention relates to an exhaust gas treatment system and method for treating exhaust gas discharged from a boiler.

 従来、火力発電設備等に設置されるボイラから排出される排ガスを処理するための排ガス処理システムが知られている。排ガス処理システムは、ボイラからの排ガスから窒素酸化物を除去する脱硝装置と、脱硝装置を通過した排ガスの熱を回収するエアヒータと、熱回収後の排ガス中の煤塵を除去する集塵機と、除塵後の排ガス中の硫黄酸化物を除去するための脱硫装置とを備えている。脱硫装置としては、石灰吸収液等を排ガスと気液接触させて排ガス中の硫黄酸化物を除去する湿式の脱硫装置が一般的に用いられる。 Conventionally, an exhaust gas treatment system for treating exhaust gas discharged from a boiler installed in a thermal power generation facility or the like is known. The exhaust gas treatment system includes a denitration device that removes nitrogen oxides from exhaust gas from a boiler, an air heater that recovers the heat of exhaust gas that has passed through the denitration device, a dust collector that removes soot and dust in the exhaust gas after heat recovery, and after dust removal And a desulfurization device for removing sulfur oxides in the exhaust gas. As the desulfurization apparatus, a wet desulfurization apparatus that removes sulfur oxide in the exhaust gas by bringing the lime absorbing liquid or the like into gas-liquid contact with the exhaust gas is generally used.

 湿式の脱硫装置から排出される排水(以下、「脱硫排水」という。)には、塩素イオン、アンモニウムイオン等のイオンや水銀など様々な種類の有害物質が多量に含まれる。このため、脱硫排水をシステム外部に放流する前に脱硫排水からこれらの有害物質を除去する必要があるが、脱硫排水中に含まれるこれら多種類の有害物質の除去処理は複雑であり、処理コストが高いという問題がある。そこで、脱硫排水の処理コストを節減すべく、脱硫排水をシステム外部に放出することなくシステム内で再利用する方法が提案されている。例えば、特許文献1には、脱硝装置、エアヒータ、集塵機、脱硫装置とが接続される主ラインの煙道から分岐して、脱硫排水を噴霧してガス化する設備を別途設置し、主ラインの煙道から排ガスの一部をこの設備内に導入し、設備内の排ガス中に脱硫排水を噴霧して蒸発させることにより有害物質を析出させた後、このガスを主ラインの煙道に戻すように構成された排ガス処理システムが開示されている。 Wastewater discharged from wet desulfurization equipment (hereinafter referred to as “desulfurization wastewater”) contains a large amount of various kinds of harmful substances such as ions such as chlorine ions and ammonium ions and mercury. For this reason, it is necessary to remove these harmful substances from the desulfurization effluent before the desulfurization effluent is discharged to the outside of the system, but the removal process of these various types of harmful substances contained in the desulfurization effluent is complicated, and the treatment cost There is a problem that is high. In order to reduce the treatment cost of the desulfurization waste water, a method for reusing the desulfurization waste water in the system without releasing it to the outside of the system has been proposed. For example, Patent Document 1 separately installs equipment for branching from a flue of a main line to which a denitration apparatus, an air heater, a dust collector, and a desulfurization apparatus are connected, and spraying and degassing desulfurization drainage. Part of the flue gas from the flue is introduced into the facility, and after desulfurization wastewater is sprayed and evaporated in the flue gas in the facility to deposit harmful substances, the gas is returned to the flue in the main line. An exhaust gas treatment system configured as described above is disclosed.

特開平9-313881号公報Japanese Patent Laid-Open No. 9-313881

 しかしながら、特許文献1の排ガス処理システムでは、主ラインの煙道から分岐して、脱硫排水を噴霧してガス化する設備を別途設置し、主ラインの煙道から排ガスの一部をこの設備内に導入し、設備内の排ガス中に脱硫排水を噴霧して蒸発させた後、このガスを主ラインの煙道内に戻す構成としているため、脱硫排水を蒸発させるための設備を別途設ける必要があり、排ガス処理システム全体が大型化するという問題がある。 However, in the exhaust gas treatment system disclosed in Patent Document 1, a facility for branching from the flue of the main line and spraying and degassing the desulfurization effluent is installed separately, and a part of the exhaust gas from the flue of the main line is installed in this facility. After desulfurization wastewater is sprayed and evaporated in the exhaust gas in the facility, this gas is returned to the flue of the main line, so it is necessary to provide a separate facility for evaporating the desulfurization wastewater. There is a problem that the whole exhaust gas treatment system is enlarged.

 また、一般的に、排ガスの処理量が増えると、それに比例して脱硫排水の量も増えるが、特許文献1の排ガス処理システムでは、脱硫排水を上記の噴霧設備の処理能力で煙道内に戻すことのできるガスの量が制限されるため、単位時間に大量の脱硫排水を処理することができず、結果として排ガスの処理量も抑えられてしまうという問題がある。 In general, as the amount of exhaust gas treatment increases, the amount of desulfurization wastewater also increases in proportion thereto. However, in the exhaust gas treatment system of Patent Document 1, the desulfurization wastewater is returned to the flue by the treatment capacity of the spray equipment. Since the amount of gas that can be used is limited, there is a problem that a large amount of desulfurization waste water cannot be treated per unit time, and as a result, the amount of exhaust gas treated is also suppressed.

 このため、排ガス処理システム全体が大型化することなく、従来に比して単位時間当たりに煙道内に戻す脱硫排水の量を増やすことが切望されている。 Therefore, it is desired to increase the amount of desulfurization drainage returned to the flue per unit time as compared with the conventional one without increasing the size of the entire exhaust gas treatment system.

 本発明は、上記に鑑みてなされたものであって、排ガス処理システム全体が大型化することなく、従来に比して単位時間当たりに煙道内に戻す脱硫排水の量を増やすことのできる排ガス処理システム及び排ガス処理方法を提供することを目的とする。 The present invention has been made in view of the above, and an exhaust gas treatment capable of increasing the amount of desulfurization wastewater returned into the flue per unit time as compared with the conventional one without increasing the size of the entire exhaust gas treatment system. It is an object to provide a system and an exhaust gas treatment method.

 上述した課題を解決し、目的を達成するために、本発明の請求項1に係る排ガス処理システムは、燃料を燃焼させるボイラと、前記ボイラからの排ガスの熱を回収するエアヒータと、熱回収後の排ガス中に含まれる硫黄酸化物を吸収液で除去する脱硫装置とを備えた排ガス処理システムにおいて、前記ボイラに燃料を供給する経路、前記ボイラの炉内部、前記ボイラと前記エアヒータとの間の煙道内部の少なくとも一箇所に、前記脱硫装置から排出される脱硫排水を供給する排水供給手段を備えることを特徴とする。 In order to solve the above-described problems and achieve the object, an exhaust gas treatment system according to claim 1 of the present invention includes a boiler that burns fuel, an air heater that recovers heat of exhaust gas from the boiler, and after heat recovery In the exhaust gas treatment system comprising a desulfurization device that removes sulfur oxides contained in the exhaust gas of the boiler with an absorbing liquid, a path for supplying fuel to the boiler, the furnace interior of the boiler, and between the boiler and the air heater A drainage supply means for supplying desulfurization drainage discharged from the desulfurization device is provided at least at one location inside the flue.

 また、本発明の請求項2に係る排ガス処理システムは、上記請求項1において、前記エアヒータの上流側に、前記ボイラからの排ガス中の窒素酸化物を除去する脱硝装置を備え、前記ボイラと前記脱硝装置との間、又は、前記脱硝装置と前記エアヒータとの間の少なくとも一方に前記排水供給手段を設けたことを特徴とする。 An exhaust gas treatment system according to claim 2 of the present invention is the exhaust gas treatment system according to claim 1, further comprising a denitration device for removing nitrogen oxides in the exhaust gas from the boiler upstream of the air heater, the boiler and the The drainage supply means is provided between at least one of a denitration device or between the denitration device and the air heater.

 また、本発明の請求項3に係る排ガス処理システムは、上記請求項2において、前記脱硝装置と並列な位置、又は、前記エアヒータと並列な位置の少なくとも一方にバイパス管を設け、前記バイパス管に前記排水供給手段を設けたことを特徴とする。 An exhaust gas treatment system according to claim 3 of the present invention is the exhaust gas treatment system according to claim 2, wherein a bypass pipe is provided at least one of a position parallel to the denitration device or a position parallel to the air heater, The waste water supply means is provided.

 また、本発明の請求項4に係る排ガス処理システムは、燃料を燃焼させるボイラと、前記ボイラからの排ガスの熱を回収するエアヒータと、熱回収後の排ガス中に含まれる硫黄酸化物を吸収液で除去する脱硫装置とを備えた排ガス処理システムにおいて、前記脱硫装置から排出される脱硫排水から有害物質を除去処理する排水処理手段と、前記ボイラに燃料を供給する経路、前記ボイラの炉内部、前記ボイラと前記エアヒータとの間の煙道内部の少なくとも一箇所に設置され前記排水処理手段で処理された処理排水を噴霧する排水供給手段と、を備えることを特徴とする。 According to a fourth aspect of the present invention, there is provided an exhaust gas treatment system that absorbs a boiler that burns fuel, an air heater that recovers heat of exhaust gas from the boiler, and sulfur oxides contained in the exhaust gas after heat recovery. In the exhaust gas treatment system comprising the desulfurization device to be removed in step, waste water treatment means for removing harmful substances from the desulfurization waste water discharged from the desulfurization device, a path for supplying fuel to the boiler, the furnace interior of the boiler, Waste water supply means for spraying treated waste water that is installed in at least one location inside the flue between the boiler and the air heater and that has been treated by the waste water treatment means.

 また、本発明の請求項5に係る排ガス処理システムは、上記請求項4において、前記エアヒータの上流側に、前記ボイラからの排ガス中の窒素酸化物を除去する脱硝装置を備え、前記ボイラと前記脱硝装置との間、又は、前記脱硝装置と前記エアヒータとの間の少なくとも一方に前記排水供給手段を設けたことを特徴とする。 An exhaust gas treatment system according to claim 5 of the present invention is the exhaust gas treatment system according to claim 4, further comprising a denitration device for removing nitrogen oxides in the exhaust gas from the boiler on the upstream side of the air heater. The drainage supply means is provided between at least one of a denitration device or between the denitration device and the air heater.

 また、本発明の請求項6に係る排ガス処理システムは、上記請求項5において、前記脱硝装置と並列な位置、又は、前記エアヒータと並列な位置の少なくとも一方にバイパス管を設け、前記バイパス管に前記排水供給手段を設けたことを特徴とする。 An exhaust gas treatment system according to claim 6 of the present invention is the exhaust gas treatment system according to claim 5, wherein a bypass pipe is provided in at least one of a position parallel to the denitration apparatus or a position parallel to the air heater, and the bypass pipe The waste water supply means is provided.

 また、本発明の請求項7に係る排ガス処理システムは、上記請求項4において、前記排水処理手段は、前記脱硫装置から排出される脱硫排水中の固体分と液体分とを分離する固液分離装置を備えることを特徴とする。 Further, the exhaust gas treatment system according to claim 7 of the present invention is the solid-liquid separation according to claim 4, wherein the waste water treatment means separates the solid content and the liquid content in the desulfurization waste water discharged from the desulfurization apparatus. A device is provided.

 また、本発明の請求項8に係る排ガス処理システムは、上記請求項4において、前記排水処理手段は、前記脱硫装置から排出される脱硫排水に含まれる水銀を除去する水銀除去装置を備えることを特徴とする。 Moreover, the exhaust gas treatment system according to claim 8 of the present invention is the exhaust gas treatment system according to claim 4, wherein the waste water treatment means includes a mercury removal device for removing mercury contained in the desulfurization waste water discharged from the desulfurization device. Features.

 また、本発明の請求項9に係る排ガス処理システムは、上記請求項4において、前記排水処理手段は、前記脱硫装置から排出される脱硫排水中に含まれるハロゲンイオンを除去するハロゲンイオン除去装置を備えることを特徴とする。 The exhaust gas treatment system according to claim 9 of the present invention is the exhaust gas treatment system according to claim 4, wherein the wastewater treatment means is a halogen ion removal device that removes halogen ions contained in the desulfurization wastewater discharged from the desulfurization device. It is characterized by providing.

 また、本発明の請求項10に係る排ガス処理方法は、燃料を燃焼させるボイラからの排ガスの熱をエアヒータにより回収した後、脱硫装置において、熱回収後の排ガス中に含まれる硫黄酸化物を吸収液で除去する排ガス処理方法において、前記ボイラに燃料を供給する経路、前記ボイラの炉内部、前記ボイラと前記エアヒータとの間の煙道内部の少なくとも一箇所に、前記脱硫装置から排出される脱硫排水を供給することを特徴とする。 In the exhaust gas treatment method according to claim 10 of the present invention, the heat of the exhaust gas from the boiler that burns the fuel is recovered by the air heater, and then the sulfur oxide contained in the exhaust gas after the heat recovery is absorbed in the desulfurization apparatus. In the exhaust gas treatment method for removing with liquid, desulfurization exhausted from the desulfurization device at least at one place in a path for supplying fuel to the boiler, inside a furnace of the boiler, and inside a flue between the boiler and the air heater It is characterized by supplying drainage.

 また、本発明の請求項11に係る排ガス処理方法は、上記請求項10において、前記エアヒータの上流側に、前記ボイラからの排ガス中の窒素酸化物を除去する脱硝装置を配置し、前記ボイラと前記脱硝装置との間、又は、前記脱硝装置と前記エアヒータとの間の少なくとも一方に前記脱硫排水を供給することを特徴とする。 An exhaust gas treatment method according to an eleventh aspect of the present invention is the exhaust gas treatment method according to the tenth aspect, wherein a denitration device for removing nitrogen oxides in the exhaust gas from the boiler is disposed upstream of the air heater, The desulfurization drainage is supplied to at least one of the denitration apparatus or between the denitration apparatus and the air heater.

 また、本発明の請求項12に係る排ガス処理方法は、上記請求項11において、前記脱硝装置と並列な位置、又は、前記エアヒータと並列な位置の少なくとも一方にバイパス管を設け、前記バイパス管の内部に前記脱硫排水を供給することを特徴とする。 An exhaust gas treatment method according to a twelfth aspect of the present invention is the exhaust gas treatment method according to the eleventh aspect, wherein a bypass pipe is provided in at least one of a position parallel to the denitration device or a position parallel to the air heater, The desulfurization waste water is supplied inside.

 また、本発明の請求項13に係る排ガス処理方法は、燃料を燃焼させるボイラからの排ガスの熱をエアヒータにより回収した後、脱硫装置において、熱回収後の排ガス中に含まれる硫黄酸化物を吸収液で除去する排ガス処理方法において、前記脱硫装置から排出される脱硫排水から有害物質を除去する排水処理を行った後、前記ボイラに燃料を供給する経路、前記ボイラの炉内部、前記ボイラと前記エアヒータとの間の煙道内部の少なくとも一箇所に、前記排水処理で処理した処理排水を供給することを特徴とする。 In the exhaust gas treatment method according to claim 13 of the present invention, after the heat of the exhaust gas from the boiler that burns the fuel is recovered by the air heater, the desulfurization device absorbs the sulfur oxide contained in the exhaust gas after the heat recovery. In the exhaust gas treatment method for removing with a liquid, after performing waste water treatment for removing harmful substances from the desulfurization waste water discharged from the desulfurization apparatus, a path for supplying fuel to the boiler, the furnace interior of the boiler, the boiler and the The treated wastewater treated by the wastewater treatment is supplied to at least one location inside the flue between the air heater and the air heater.

 また、本発明の請求項14に係る排ガス処理方法は、上記請求項13において、前記エアヒータの上流側に、前記ボイラからの排ガス中の窒素酸化物を除去する脱硝装置を配置し、前記ボイラと前記脱硝装置との間、又は、前記脱硝装置と前記エアヒータとの間の少なくとも一方に前記処理排水を供給することを特徴とする。 The exhaust gas treatment method according to claim 14 of the present invention is the exhaust gas treatment method according to claim 13, wherein a denitration device for removing nitrogen oxides in the exhaust gas from the boiler is disposed upstream of the air heater, The treated waste water is supplied to at least one of the denitration device or between the denitration device and the air heater.

 また、本発明の請求項15に係る排ガス処理方法は、上記請求項14において、前記脱硝装置と並列な位置、又は、前記エアヒータと並列な位置の少なくとも一方にバイパス管を設け、前記バイパス管の内部に前記処理排水を供給することを特徴とする。 An exhaust gas treatment method according to claim 15 of the present invention is the exhaust gas treatment method according to claim 14, wherein a bypass pipe is provided at at least one of a position parallel to the denitration device or a position parallel to the air heater, The treatment waste water is supplied inside.

 また、本発明の請求項16に係る排ガス処理方法は、上記請求項13において、前記排水処理は、前記脱硫装置から排出される脱硫排水中の固体分と液体分とを分離する固液分離処理を含むことを特徴とする。 The exhaust gas treatment method according to claim 16 of the present invention is the solid-liquid separation process according to claim 13, wherein the waste water treatment separates a solid content and a liquid content in the desulfurization waste water discharged from the desulfurization apparatus. It is characterized by including.

 また、本発明の請求項17に係る排ガス処理方法は、上記請求項13において、前記排水処理は、前記脱硫装置から排出される脱硫排水に含まれる水銀を除去する水銀除去処理を含むことを特徴とする。 The exhaust gas treatment method according to claim 17 of the present invention is the exhaust gas treatment method according to claim 13, wherein the waste water treatment includes a mercury removal treatment for removing mercury contained in the desulfurization waste water discharged from the desulfurization apparatus. And

 また、本発明の請求項18に係る排ガス処理方法は、上記請求項13において、前記排水処理は、前記脱硫装置から排出される脱硫排水中に含まれるハロゲンイオンを除去するハロゲンイオン除去処理を含むことを特徴とする。 The exhaust gas treatment method according to claim 18 of the present invention is the exhaust gas treatment method according to claim 13, wherein the waste water treatment includes a halogen ion removal treatment for removing halogen ions contained in the desulfurization waste water discharged from the desulfurization apparatus. It is characterized by that.

 本発明の排ガス処理システム及び排ガス処理方法によれば、ボイラに燃料を供給する経路、ボイラの炉内部、ボイラとエアヒータとの間の煙道内部の少なくとも一箇所に脱硫排水を直接噴霧する構成としたので、従来のように脱硫排水を蒸発させてガス化する装置を別途設ける必要がない。その結果、排ガス処理システムを大型化することなく、脱硫装置からの脱硫排水のうちシステム外部に放出する量を低減することが可能となる。 According to the exhaust gas treatment system and the exhaust gas treatment method of the present invention, a structure for spraying desulfurization wastewater directly to at least one place in the path for supplying fuel to the boiler, the furnace interior of the boiler, and the flue between the boiler and the air heater; Therefore, it is not necessary to separately provide a device for evaporating and degassing the desulfurized waste water as in the conventional case. As a result, it is possible to reduce the amount of desulfurization effluent from the desulfurization apparatus that is discharged outside the system without increasing the size of the exhaust gas treatment system.

 また、ボイラ内部やボイラとエアヒータとの間の煙道内の排ガスは、エアヒータで熱回収される前の高温ガスであるから、ボイラ内部や煙道内に多量の脱硫排水を蒸発させることができる。このため、従来に比して単位時間当たりに煙道内に戻す排水の量を増やすことができる。その結果、従来に比して処理できる脱硫排水の量を増やすことができ、結果として、単位時間当たりの排ガスの処理量を増やすことができる。 Moreover, since the exhaust gas in the flue between the boiler and between the boiler and the air heater is a high-temperature gas before heat recovery by the air heater, a large amount of desulfurization waste water can be evaporated in the boiler or in the flue. For this reason, compared with the past, the quantity of the waste_water | drain which returns in a flue per unit time can be increased. As a result, it is possible to increase the amount of desulfurization waste water that can be treated as compared with the conventional case, and as a result, it is possible to increase the amount of exhaust gas treated per unit time.

 また、本発明の排ガス処理システム及び排ガス処理方法によれば、脱硫装置から排出される脱硫排水から有害物質を除去処理する排水処理を行い、ボイラに燃料を供給する経路、ボイラの炉内部、ボイラとエアヒータとの間の煙道内部の少なくとも一箇所に、、排水処理で処理された処理排水を直接噴霧する構成としたので、煙道内部における排ガス中の有害物質濃度の増加を防止することができる。 Further, according to the exhaust gas treatment system and the exhaust gas treatment method of the present invention, a waste water treatment for removing harmful substances from the desulfurization waste water discharged from the desulfurization apparatus, a route for supplying fuel to the boiler, the boiler interior, the boiler Because the treated wastewater treated in the wastewater treatment is sprayed directly to at least one place inside the flue between the air heater and the air heater, it is possible to prevent an increase in the concentration of harmful substances in the exhaust gas inside the flue it can.

図1は、実施例1に係る排ガス処理システムの概略構成図である。FIG. 1 is a schematic configuration diagram of an exhaust gas treatment system according to a first embodiment. 図2は、実施例2に係る排ガス処理システムの概略構成図である。FIG. 2 is a schematic configuration diagram of an exhaust gas treatment system according to a second embodiment. 図3は、実施例3に係る排ガス処理システムの概略構成図である。FIG. 3 is a schematic configuration diagram of an exhaust gas treatment system according to a third embodiment. 図4は、実施例4に係る排ガス処理システムの概略構成図である。FIG. 4 is a schematic configuration diagram of an exhaust gas treatment system according to a fourth embodiment. 図5は、実施例5に係る排ガス処理システムの概略構成図である。FIG. 5 is a schematic configuration diagram of an exhaust gas treatment system according to a fifth embodiment.

 以下、この発明につき図面を参照しつつ詳細に説明する。なお、この実施例によりこの発明が限定されるものではない。また、下記実施例における構成要素には、当業者が容易に想定できるもの、あるいは実質的に同一のものが含まれる。 Hereinafter, the present invention will be described in detail with reference to the drawings. Note that the present invention is not limited to the embodiments. In addition, constituent elements in the following embodiments include those that can be easily assumed by those skilled in the art or those that are substantially the same.

 図1は、実施例1に係る排ガス処理システムの概略構成図である。図1に例示される排ガス処理システム10Aは、石炭を燃料として使用する石炭焚きボイラや重油を燃料として使用する重油焚きボイラ等のボイラ11からの排ガス17から、窒素酸化物(NO)、硫黄酸化物(SO)、水銀(Hg)等の有害物質を除去する装置である。 FIG. 1 is a schematic configuration diagram of an exhaust gas treatment system according to a first embodiment. An exhaust gas treatment system 10A illustrated in FIG. 1 includes nitrogen oxide (NO x ), sulfur from exhaust gas 17 from a boiler 11 such as a coal fired boiler using coal as a fuel or a heavy oil fired boiler using heavy oil as a fuel. This is a device for removing harmful substances such as oxide (SO x ) and mercury (Hg).

 排ガス処理システム10Aは、ボイラ11からの排ガス17中の窒素酸化物を除去する脱硝装置12と、脱硝装置12を通過した排ガス17の熱を回収するエアヒータ13と、熱回収後の排ガス17中の煤塵を除去する集塵機14と、煤塵が除去された後の排ガス17中の硫黄酸化物を湿式で除去する脱硫装置15、及び、脱硫装置15から排出される脱硫排水28を、ボイラ11に燃料Fを供給する経路、ボイラ11の炉内部、ボイラ11からエアヒータ13に至る煙道内部の少なくとも一箇所に供給する排水噴霧装置16とを備えて構成されている。これにより、従来に比して単位時間当たりにボイラ11、煙道D内に戻す脱硫排水の量を増やすことを可能としている。 The exhaust gas treatment system 10A includes a denitration device 12 that removes nitrogen oxides in the exhaust gas 17 from the boiler 11, an air heater 13 that recovers the heat of the exhaust gas 17 that has passed through the denitration device 12, and an exhaust gas 17 after the heat recovery. A dust collector 14 that removes soot, a desulfurization device 15 that removes sulfur oxide in the exhaust gas 17 after the dust is removed, and a desulfurization waste water 28 that is discharged from the desulfurization device 15 are supplied to the boiler 11 as fuel F. And a waste water spray device 16 for supplying at least one place inside the flue from the boiler 11 to the air heater 13. Thereby, it is possible to increase the amount of desulfurization drainage returned to the boiler 11 and the flue D per unit time as compared with the conventional case.

 脱硝装置12は、ボイラ11からの排ガス17中の窒素酸化物を除去する装置であり、その内部に脱硝触媒層(図示せず)を有している。脱硝触媒層の前流には還元剤注入器(図示せず)が配置され、この還元剤注入器から排ガス17に還元剤が注入される。ここで還元剤としては、例えばアンモニア、尿素、塩化アンモニウムなどが用いられる。脱硝装置12に導入された排ガス17は、脱硝触媒層と接触することにより、排ガス17中の窒素酸化物が窒素ガス(N)と水(HO)に分解・除去される。また、排ガス中の塩素(Cl)分が多くなると、水に可溶な2価の塩化水銀の割合が多くなり、後述する脱硫装置15で水銀が捕集しやすくなる。 The denitration device 12 is a device that removes nitrogen oxides in the exhaust gas 17 from the boiler 11, and has a denitration catalyst layer (not shown) therein. A reducing agent injector (not shown) is disposed upstream of the denitration catalyst layer, and the reducing agent is injected into the exhaust gas 17 from the reducing agent injector. Here, for example, ammonia, urea, ammonium chloride or the like is used as the reducing agent. The exhaust gas 17 introduced into the denitration device 12 comes into contact with the denitration catalyst layer, whereby nitrogen oxides in the exhaust gas 17 are decomposed and removed into nitrogen gas (N 2 ) and water (H 2 O). Further, when the chlorine (Cl) content in the exhaust gas increases, the proportion of divalent mercury chloride soluble in water increases, and mercury is easily collected by the desulfurization apparatus 15 described later.

 なお、上記の脱硝装置12は必須のものではなく、ボイラ11からの排ガス17中の窒素酸化物濃度や水銀濃度が微量、あるいは、排ガス17中にこれらの物質が含まれない場合には、脱硝装置12を省略することも可能である。 The denitration device 12 is not essential, and when the nitrogen oxide concentration or mercury concentration in the exhaust gas 17 from the boiler 11 is very small, or when these substances are not contained in the exhaust gas 17, denitration is performed. It is also possible to omit the device 12.

 エアヒータ13は、脱硝装置12で窒素酸化物が除去された後の排ガス17中の熱を回収する熱交換器である。脱硝装置12を通過した排ガス17の温度は350℃~400℃程度と高温であるため、エアヒータ13により高温の排ガス17と常温の燃焼用空気との間で熱交換を行う。熱交換により高温となった燃焼用空気は、ボイラ11に供給される。一方、常温の燃焼用空気との熱交換を行った排ガス17は150℃程度まで冷却される。 The air heater 13 is a heat exchanger that recovers heat in the exhaust gas 17 after nitrogen oxides are removed by the denitration device 12. Since the temperature of the exhaust gas 17 that has passed through the denitration device 12 is as high as about 350 ° C. to 400 ° C., heat exchange is performed between the high temperature exhaust gas 17 and normal temperature combustion air by the air heater 13. The combustion air that has reached a high temperature due to heat exchange is supplied to the boiler 11. On the other hand, the exhaust gas 17 that has exchanged heat with the combustion air at normal temperature is cooled to about 150 ° C.

 集塵機14は、熱回収後の排ガス17中の煤塵を除去するものである。集塵機14としては遠心力集塵器、濾過式集塵器、電気集塵器等が挙げられるが、特に限定されない。 The dust collector 14 removes the dust in the exhaust gas 17 after heat recovery. Examples of the dust collector 14 include a centrifugal dust collector, a filtration dust collector, and an electric dust collector, but are not particularly limited.

 脱硫装置15は、煤塵が除去された後の排ガス17中の硫黄酸化物を湿式で除去する装置である。この脱硫装置15では、アルカリ吸収液として石灰スラリー20(水に石灰石粉末を溶解させた水溶液)が用いられ、装置内の温度は30~50℃程度に調節されている。石灰スラリー20は、石灰スラリー供給装置21から脱硫装置15の塔底部22に供給される。脱硫装置15の塔底部22に供給された石灰スラリー20は、図示しない吸収液送給ラインを介して脱硫装置15内の複数のノズル23に送られ、ノズル23から塔頂部24側に向かって噴出される。脱硫装置15の塔底部22側から上昇してくる排ガス17がノズル23から噴出する石灰スラリー20と気液接触することにより、排ガス17中の硫黄酸化物及び塩化水銀が石灰スラリー20により吸収され、排ガス17から分離、除去される。石灰スラリー20により浄化された排ガス17は、浄化ガス26として脱硫装置15の塔頂部24側より排出され、煙突27から系外に排出される。 The desulfurization device 15 is a device that removes sulfur oxides in the exhaust gas 17 after the dust is removed by a wet process. In this desulfurization apparatus 15, lime slurry 20 (an aqueous solution in which limestone powder is dissolved in water) is used as an alkali absorbing liquid, and the temperature in the apparatus is adjusted to about 30 to 50 ° C. The lime slurry 20 is supplied from the lime slurry supply device 21 to the tower bottom 22 of the desulfurization device 15. The lime slurry 20 supplied to the tower bottom 22 of the desulfurization apparatus 15 is sent to a plurality of nozzles 23 in the desulfurization apparatus 15 via an absorption liquid supply line (not shown), and ejected from the nozzle 23 toward the tower top 24 side. Is done. When the exhaust gas 17 rising from the tower bottom 22 side of the desulfurization apparatus 15 comes into gas-liquid contact with the lime slurry 20 ejected from the nozzle 23, sulfur oxide and mercury chloride in the exhaust gas 17 are absorbed by the lime slurry 20, It is separated from the exhaust gas 17 and removed. The exhaust gas 17 purified by the lime slurry 20 is discharged from the tower top 24 side of the desulfurization device 15 as the purified gas 26 and is discharged out of the system from the chimney 27.

 脱硫装置15の内部において、排ガス17中の硫黄酸化物SOは石灰スラリー19と下記式(1)で表される反応を生じる。
CaCO+SO+0.5HO → CaSO・0.5HO +CO・・・(1)
Inside the desulfurization device 15, the sulfur oxide SO x in the exhaust gas 17 causes a reaction represented by the lime slurry 19 and the following formula (1).
CaCO 3 + SO 2 + 0.5H 2 O → CaSO 3 · 0.5H 2 O + CO 2 (1)

 さらに、排ガス17中のSOを吸収した石灰スラリー20は、脱硫装置15の塔底部22に供給される空気(図示せず)により酸化処理され、空気と下記式(2)で表される反応を生じる。
CaSO・0.5HO+0.5O+1.5HO → CaSO・2HO・・・(2)
 このようにして、排ガス17中のSOは、脱硫装置15において石膏CaSO・2HOの形で捕獲される。
Further, the lime slurry 20 that has absorbed SO x in the exhaust gas 17 is oxidized by air (not shown) supplied to the tower bottom 22 of the desulfurization apparatus 15, and the reaction represented by the air and the following formula (2) is performed. Produce.
CaSO 3 · 0.5H 2 O + 0.5O 2 + 1.5H 2 O → CaSO 4 · 2H 2 O (2)
In this way, SO x in the exhaust gas 17 is captured in the form of gypsum CaSO 4 .2H 2 O in the desulfurization apparatus 15.

 また、上記のように、石灰スラリー20は、脱硫装置15の塔底部22に貯留した液を揚水したものが用いられるが、この揚水される石灰スラリーには、脱硫装置15の稼働に伴い、反応式(1)、(2)により石膏CaSO・2HOが混合される。以下では、この揚水される石灰石膏スラリー(石膏が混合された石灰スラリー)を吸収液とよぶ。 Further, as described above, the lime slurry 20 is obtained by pumping the liquid stored in the tower bottom 22 of the desulfurization device 15, and the lime slurry pumped up reacts with the operation of the desulfurization device 15. Gypsum CaSO 4 · 2H 2 O is mixed according to the formulas (1) and (2). Below, this lime-gypsum slurry (lime slurry mixed with gypsum) to be pumped is called an absorbent.

 脱硫に用いた吸収液(石灰石膏スラリー)は、脱硫排水28として脱硫装置15の塔底部22から外部に排出され、後述する排水ライン29を介して排水タンク31に貯留される。この脱硫排水28には、石膏の他、水銀等の重金属やCl、Br,I,F等のハロゲンイオンが含まれている。 The absorption liquid (lime gypsum slurry) used for desulfurization is discharged to the outside from the tower bottom 22 of the desulfurization device 15 as desulfurization drainage 28 and is stored in the drainage tank 31 through a drainage line 29 described later. In addition to gypsum, the desulfurization effluent 28 contains heavy metals such as mercury and halogen ions such as Cl , Br , I and F .

 上述したボイラ11、脱硝装置12、エアヒータ13、集塵機14、脱硫装置15は、一本の煙道Dにより接続されている。また、脱硝装置12と並列な位置には、脱硝装置12の上流側と下流側の煙道Dを接続するバイパス管32が設けられている。同様にして、エアヒータ13と並列な位置には、エアヒータ13の上流側と下流側の煙道Dを接続するバイパス管33が設けられている。上記構成とすることで、各バイパス管32,33の内部を流通する排ガス17中にも脱硫排水28を噴霧することができるようになっている。各バイパス管32、33は、その内部を流通する排ガス量が煙道Dを流通する排ガス量の数%程度となるように構成されている。 The boiler 11, the denitration device 12, the air heater 13, the dust collector 14, and the desulfurization device 15 described above are connected by a single flue D. Further, a bypass pipe 32 that connects the upstream side and the downstream side flue D of the denitration device 12 is provided at a position parallel to the denitration device 12. Similarly, a bypass pipe 33 that connects the upstream side and the downstream side flue D of the air heater 13 is provided at a position parallel to the air heater 13. By setting it as the said structure, the desulfurization waste_water | drain 28 can be sprayed also in the waste gas 17 which distribute | circulates the inside of each bypass pipe 32,33. Each of the bypass pipes 32 and 33 is configured such that the amount of exhaust gas flowing through the inside thereof is about several percent of the amount of exhaust gas flowing through the flue D.

 排水噴霧装置16は、脱硫装置15から排出される脱硫排水(石膏スラリー)28を排水タンク31に送液する排水ライン29と、脱硫排水28を貯留する排水タンク31と、排水タンク31に接続され、排水タンク31に貯留された脱硫排水28をボイラ11に燃料Fを供給する経路と、ボイラ11の炉内部と、煙道Dの内部及びバイパス管32,33の内部に供給する複数の排水供給管(排水供給手段)P0~P5とを備えている。排水供給管P1~P5の先端には、脱硫排水28を噴霧するノズルN1~N5が取り付けられている。 The drain spray device 16 is connected to the drain line 29 for sending the desulfurization drainage (gypsum slurry) 28 discharged from the desulfurization device 15 to the drain tank 31, the drain tank 31 for storing the desulfurization drain 28, and the drain tank 31. A plurality of drainage supplies for supplying fuel F to the boiler 11 from the desulfurization drainage 28 stored in the drainage tank 31, inside the furnace of the boiler 11, inside the flue D and inside the bypass pipes 32 and 33 Pipes (drainage supply means) P0 to P5 are provided. Nozzles N1 to N5 for spraying the desulfurized waste water 28 are attached to the tips of the drainage supply pipes P1 to P5.

 排水供給管P1~P5は、エアヒータ13により熱が回収される前の高温の排ガス17が流通する位置、すなわち、エアヒータ13よりも上流側に設置される。図1に示す例では、排水供給管P1はボイラ11に接続され、ノズルN1はボイラ11の炉内部に設置されている。具体的には、ノズルN1は、炉の側面や炉の上部の炉壁に設置され、当該ノズルN1から炉の中央部の火炎部分又は火炎の上方に向かって脱硫排水28が噴射される。また、排水供給管P2はボイラ11の出口と脱硝装置12の間の煙道Dに接続され、ノズルN2は煙道Dの内部に設置されている。また、排水供給管P3は、脱硝装置12の上流側の煙道Dと下流側の煙道Dを接続するバイパス管32に接続され、ノズルN3はバイパス管32の内部に設置されている。また、排水供給管P4は、脱硝装置12とエアヒータ13との間の煙道Dに接続され、ノズルN4は煙道Dの内部に設置されている。また、排水供給管P5は、エアヒータ13の上流側の煙道Dと下流側の煙道Dを接続するバイパス管33に接続され、ノズルN5はバイパス管33の内部に設置されている。 The drainage supply pipes P1 to P5 are installed at a position where the high-temperature exhaust gas 17 before the heat is recovered by the air heater 13, that is, upstream of the air heater 13. In the example shown in FIG. 1, the drainage supply pipe P <b> 1 is connected to the boiler 11, and the nozzle N <b> 1 is installed inside the furnace of the boiler 11. Specifically, the nozzle N1 is installed on the side wall of the furnace or the furnace wall at the top of the furnace, and the desulfurization waste water 28 is sprayed from the nozzle N1 toward the flame portion in the center of the furnace or above the flame. Further, the drainage supply pipe P2 is connected to the flue D between the outlet of the boiler 11 and the denitration apparatus 12, and the nozzle N2 is installed inside the flue D. Further, the drainage supply pipe P3 is connected to a bypass pipe 32 connecting the upstream flue D and the downstream flue D of the denitration apparatus 12, and the nozzle N3 is installed inside the bypass pipe 32. The drainage supply pipe P4 is connected to a flue D between the denitration device 12 and the air heater 13, and the nozzle N4 is installed inside the flue D. Further, the drainage supply pipe P5 is connected to a bypass pipe 33 connecting the upstream flue D and the downstream flue D of the air heater 13, and the nozzle N5 is installed inside the bypass pipe 33.

 ノズルN1~N5としては、例えば二流体ノズル、ロータリアトマイザ等が用いられる。また、ノズルN1~N5のミスト径は、最大粒径が200μm以下、平均粒径が30~70μmとするのが好ましい。これにより、排ガス17との接触効率が向上し、蒸発効率の向上を図ることができる。 As the nozzles N1 to N5, for example, a two-fluid nozzle, a rotary atomizer or the like is used. The mist diameters of the nozzles N1 to N5 are preferably a maximum particle diameter of 200 μm or less and an average particle diameter of 30 to 70 μm. Thereby, the contact efficiency with the exhaust gas 17 is improved, and the evaporation efficiency can be improved.

 ノズルN1が設置されるボイラ11の炉内のガス温度は1400℃~1600℃程度と最も高温であるため、最も多くの脱硫排水28を蒸発させることが可能である。また、ノズルN2が設置されるボイラ11の出口と脱硝装置12との間の煙道D内部の排ガス温度は500℃程度、ノズルN4が設置される脱硝装置12とエアヒータ13との間の煙道D内部、及び、ノズルN3、N5が設置されるバイパス管32,33の排ガス温度はいずれも350℃~400℃程度であり、ボイラ11の炉内部よりも温度は低下するものの、脱硫排水28を確実に蒸発させることができる。一方、エアヒータ13を通過した排ガス17の温度は150℃程度まで低下し、脱硫排水28を十分に蒸発させることができない。 Since the gas temperature in the furnace of the boiler 11 in which the nozzle N1 is installed is the highest temperature of about 1400 ° C. to 1600 ° C., it is possible to evaporate the most desulfurization waste water 28. Further, the exhaust gas temperature inside the flue D between the outlet of the boiler 11 where the nozzle N2 is installed and the denitration device 12 is about 500 ° C., and the flue between the denitration device 12 where the nozzle N4 is installed and the air heater 13 The exhaust gas temperature inside D and the bypass pipes 32 and 33 where the nozzles N3 and N5 are installed are both about 350 ° C. to 400 ° C. Although the temperature is lower than the inside of the furnace of the boiler 11, It can be reliably evaporated. On the other hand, the temperature of the exhaust gas 17 that has passed through the air heater 13 decreases to about 150 ° C., and the desulfurized waste water 28 cannot be sufficiently evaporated.

 また、排水供給管P0は、ボイラ11に燃料Fを供給する経路に設置されている。ここで、ボイラ11に燃料Fを供給する経路とは、具体的には、燃料供給装置(図示せず)の内部や、燃料供給装置とボイラ11とを接続する配管等である。排水供給管P0から燃料Fに供給された脱硫排水28は燃料Fと混合され、燃料Fとともにボイラ11に投入された後、ボイラ内で蒸発する。 Further, the drainage supply pipe P0 is installed in a path for supplying the fuel F to the boiler 11. Here, the path for supplying the fuel F to the boiler 11 is specifically the inside of a fuel supply apparatus (not shown), piping for connecting the fuel supply apparatus and the boiler 11, or the like. The desulfurization waste water 28 supplied to the fuel F from the waste water supply pipe P0 is mixed with the fuel F, and after being put into the boiler 11 together with the fuel F, it evaporates in the boiler.

 上記の排水供給管P0~P5にはそれぞれ開閉バルブV0~V5が設置され、これらの開閉バルブV0~V5の開閉量を制御することにより、排水供給管P0~P5に供給される脱硫排水28の流量が調整される。そして、排水タンク31に貯留される脱硫排水28は、排水供給管P1~P5を通過して各ノズルN1~N5からボイラ11の炉内部、煙道D内部、バイパス管32,33内部の高温の排ガス17中にそれぞれ噴霧されるとともに、排水供給管P0を通過してボイラ11に燃料Fを供給する経路に供給される。 The drainage supply pipes P0 to P5 are provided with opening / closing valves V0 to V5, respectively. By controlling the opening / closing amounts of these opening / closing valves V0 to V5, the desulfurization drainage 28 supplied to the drainage supply pipes P0 to P5 is controlled. The flow rate is adjusted. The desulfurization drainage 28 stored in the drainage tank 31 passes through the drainage supply pipes P1 to P5 and passes through the nozzles N1 to N5 to the high temperature inside the furnace 11 of the boiler 11, the flue D, and the bypass pipes 32 and 33. The fuel is sprayed into the exhaust gas 17 and supplied to a path for supplying the fuel F to the boiler 11 through the drain supply pipe P0.

 ノズルN1~N5から高温の排ガス17中に噴霧された脱硫排水28は、蒸発して水蒸気となり、その後、排ガス17とともに脱硫装置15内に送られる。脱硫装置15内の温度は30℃~50℃程度であるため、脱硫装置15内に導入された水蒸気のほとんどは液化し、塔底部22の石灰スラリー20と混合される。一方、液化しなかった水蒸気は、浄化ガス26とともに煙突27から排出される。 The desulfurization waste water 28 sprayed into the high-temperature exhaust gas 17 from the nozzles N1 to N5 evaporates to become water vapor, and then is sent into the desulfurization device 15 together with the exhaust gas 17. Since the temperature in the desulfurization apparatus 15 is about 30 ° C. to 50 ° C., most of the water vapor introduced into the desulfurization apparatus 15 is liquefied and mixed with the lime slurry 20 at the tower bottom 22. On the other hand, the water vapor that has not been liquefied is discharged from the chimney 27 together with the purified gas 26.

 このように、エアヒータ13により熱が回収される前の高温の排ガス17中に脱硫排水28を直接噴霧するようにしたことで、脱硫排水28の噴霧量が多くても確実に脱硫排水28を蒸発させることが可能となるため、従来に比して単位時間当たりに煙道D内に戻す脱硫排水28の量を増やすことができるようになる。その結果、脱硫装置15から排出される脱硫排水28の全量を煙道D内に戻し、系外に排出しない完全無排水化を実現することが可能となる。 In this way, the desulfurization waste water 28 is directly sprayed into the high-temperature exhaust gas 17 before the heat is recovered by the air heater 13, so that the desulfurization waste water 28 is surely evaporated even when the spray amount of the desulfurization waste water 28 is large. Therefore, it is possible to increase the amount of the desulfurization waste water 28 returned into the flue D per unit time as compared with the conventional case. As a result, the entire amount of the desulfurization waste water 28 discharged from the desulfurization device 15 is returned into the flue D, and it is possible to achieve complete drainage without discharging outside the system.

 また、排ガス17の処理量に比例して脱硫装置15から排出される脱硫排水28の量も増えるから、単位時間当たりに煙道D内に戻す脱硫排水28の量を増大させた結果、単位時間に処理できる排水の量が増加し、結果として従来に比して単位時間当たりの排ガスの処理量を増やすことが可能となる。 Further, since the amount of the desulfurization waste water 28 discharged from the desulfurization device 15 increases in proportion to the treatment amount of the exhaust gas 17, the amount of the desulfurization waste water 28 returned into the flue D per unit time is increased. As a result, the amount of exhaust gas treated per unit time can be increased as compared with the conventional method.

 また、本実施例では、脱硝装置12の上流側と下流側の煙道Dを接続するバイパス管32を設けるとともに、エアヒータ13の上流側と下流側の煙道Dを接続するバイパス管33を設け、これらのバイパス管32、33の内部の排ガス17中に脱硫排水28を噴霧し、蒸発させている。このため、脱硫排水28の蒸発に伴い発生する灰等の乾燥粒子が脱硝装置12やエアヒータ13の中を通過することにより、これらの装置の働きを低下させるおそれがある場合に、各バイパス管32、33を介して乾燥粒子を効率よく脱硝装置12及びエアヒータ13の下流側に搬送することができる。 In this embodiment, a bypass pipe 32 that connects the upstream and downstream flues D of the denitration apparatus 12 is provided, and a bypass pipe 33 that connects the upstream and downstream flues D of the air heater 13 is provided. The desulfurization waste water 28 is sprayed and evaporated in the exhaust gas 17 inside these bypass pipes 32 and 33. For this reason, when the dry particles such as ash generated along with the evaporation of the desulfurization waste water 28 pass through the denitration device 12 and the air heater 13, the functions of these devices may be reduced. , 33 can efficiently transport the dry particles to the downstream side of the denitration device 12 and the air heater 13.

 また、上記のように、煙道Dの場所により排ガス17の温度が異なり、脱硫排水28の蒸発効率も異なる。そこで、乾燥粒子の搬送効率や排ガス17の蒸発効率等を考慮した上で、バルブV0~V5の開閉量を最適化する。 Further, as described above, the temperature of the exhaust gas 17 varies depending on the location of the flue D, and the evaporation efficiency of the desulfurization waste water 28 also varies. Therefore, the open / close amounts of the valves V0 to V5 are optimized in consideration of the dry particle transport efficiency, the exhaust gas 17 evaporation efficiency, and the like.

 なお、図1に示した排水噴霧装置16の構成は一例であり、排水供給管P0~P5の設置本数及び設置位置はこれに限定されるものではなく、脱硫排水28の量や排ガス17の種類等に応じて適宜変更することができる。すなわち、ボイラ11に燃料Fを供給する経路、ボイラ11の炉内部、ボイラ11の出口からエアヒータ13の入口までの煙道D、バイパス管32,33のうち、少なくとも一箇所に設置されればよい。 The configuration of the waste water spray device 16 shown in FIG. 1 is an example, and the number and location of the drainage supply pipes P0 to P5 are not limited to this. The amount of the desulfurization drainage 28 and the type of the exhaust gas 17 are not limited thereto. It can change suitably according to etc. In other words, the fuel F may be installed in at least one of the path for supplying the fuel F to the boiler 11, the furnace interior of the boiler 11, the flue D from the outlet of the boiler 11 to the inlet of the air heater 13, and the bypass pipes 32 and 33. .

 また、脱硫排水28に含まれる有害物質・固形分が微量であり、脱硝装置12やエアヒータ13の上流側の煙道D内に脱硫排水28を噴霧しても、脱硝装置12やエアヒータ13の働きを低下させるおそれがない場合には、必ずしもバイパス管32,33を設ける必要はない。また、必ずしもバイパス管32,33の両方を設ける必要はなく、どちらか一方を設けた構成としてもよい。 Further, even if the desulfurization drainage 28 is sprayed into the flue D on the upstream side of the denitration device 12 and the air heater 13 because the harmful substances and solids contained in the desulfurization drainage 28 are very small, the function of the denitration device 12 and the air heater 13 is achieved. When there is no possibility of lowering the flow rate, the bypass pipes 32 and 33 are not necessarily provided. Further, it is not always necessary to provide both the bypass pipes 32 and 33, and either one may be provided.

 さらに、図1に示した排水噴霧装置16では、脱硫排水28を排水タンク31に一旦貯留し、排水タンク31から脱硫排水28を排水供給管P0~P5に供給する構成としたが、脱硫装置15から排出された脱硫排水28を直接、排水供給管P0~P5に供給する構成としてもよい。 Further, in the drain spray device 16 shown in FIG. 1, the desulfurization drain 28 is temporarily stored in the drain tank 31, and the desulfurization drain 28 is supplied from the drain tank 31 to the drain supply pipes P0 to P5. The desulfurization waste water 28 discharged from the pipe may be directly supplied to the drain supply pipes P0 to P5.

 以上説明したように、実施例1の排ガス処理システム10Aでは、ボイラ11に燃料Fを供給する経路、ボイラ11の炉内部、ボイラ11からエアヒータ13に至る煙道内部の少なくとも一箇所に、脱硫装置15から排出される脱硫排水28を供給する排水供給管P0~P5を設置し、当該排水供給管P0~P5により脱硫排水28を直接供給する構成としている。上記構成としたことで、従来のように脱硫排水をガス化するための設備を別途設ける必要がないため、排ガス処理システム全体が大型化することなく、系外に排出する脱硫排水28の量を低減させることができる。 As described above, in the exhaust gas treatment system 10A of the first embodiment, the desulfurization device is provided in at least one place inside the flue from the boiler 11 to the air heater 13 in the path for supplying the fuel F to the boiler 11, the furnace inside the boiler 11, and the air heater 13. The drainage supply pipes P0 to P5 for supplying the desulfurization drainage 28 discharged from the pipe 15 are installed, and the desulfurization drainage 28 is directly supplied through the drainage supply pipes P0 to P5. With the above configuration, there is no need to separately provide equipment for gasifying the desulfurization drainage as in the prior art, so the amount of the desulfurization drainage 28 discharged outside the system is reduced without increasing the size of the entire exhaust gas treatment system. Can be reduced.

 さらに、エアヒータ13により熱が回収される前の高温の排ガス17中に脱硫排水28を直接噴霧する構成としているため、脱硫排水28の噴霧量が多くても確実に脱硫排水28を蒸発させることが可能となり、従来に比して単位時間当たりに煙道D内に戻す脱硫排水28の量を増やすことができるようになる。その結果、脱硫装置15から排出される脱硫排水28の全量を煙道D内に戻し、系外に排出しない完全無排水化を実現することが可能となる。また、従来に比して単位時間当たりに煙道D内に戻す脱硫排水28の量を増大させた結果、処理できる脱硫排水28の量も増えることとなり、結果として、従来に比して単位時間当たりの排ガスの処理量を増やすことができる。 Furthermore, since the desulfurization waste water 28 is directly sprayed into the high-temperature exhaust gas 17 before heat is recovered by the air heater 13, the desulfurization waste water 28 can be reliably evaporated even if the spray amount of the desulfurization waste water 28 is large. It becomes possible, and it becomes possible to increase the amount of the desulfurization waste water 28 returned into the flue D per unit time as compared with the conventional case. As a result, the entire amount of the desulfurization waste water 28 discharged from the desulfurization device 15 is returned into the flue D, and it is possible to achieve complete drainage without discharging outside the system. Further, as a result of increasing the amount of the desulfurization waste water 28 returned into the flue D per unit time as compared with the conventional case, the amount of the desulfurization waste water 28 that can be treated also increases. The processing amount of exhaust gas per hit can be increased.

 また、脱硝装置12の上流側と下流側の煙道Dを接続するバイパス管32を設け、このバイパス管32内部の排ガス17中に脱硫排水28を噴霧し、蒸発させるようにしたので、脱硫排水28の蒸発に伴い発生する灰等の乾燥粒子を、バイパス管32を介して効率的に脱硝装置12の下流側に搬送ことができる。同様に、エアヒータ13の上流側と下流側の煙道Dを接続するバイパス管33を設け、このバイパス管33内部の排ガス17中に脱硫排水28を噴霧し、蒸発させるようにしたので、脱硫排水28の蒸発に伴い発生する乾燥粒子を、バイパス管33を介して効率的にエアヒータ13の下流側に搬送することができる。 In addition, since the bypass pipe 32 connecting the upstream side and the downstream side flue D of the denitration device 12 is provided and the desulfurization drainage 28 is sprayed and evaporated in the exhaust gas 17 inside the bypass pipe 32, the desulfurization drainage Dry particles such as ash generated by the evaporation of 28 can be efficiently conveyed to the downstream side of the denitration apparatus 12 via the bypass pipe 32. Similarly, the bypass pipe 33 connecting the upstream side and the downstream side flue D of the air heater 13 is provided, and the desulfurization waste water 28 is sprayed and evaporated in the exhaust gas 17 inside the bypass pipe 33. The dry particles generated with the evaporation of 28 can be efficiently conveyed to the downstream side of the air heater 13 via the bypass pipe 33.

 なお、図1に示した例では、脱硫装置15から排出される脱硫排水28の全量を、ボイラ11に燃料Fを供給する経路、ボイラ11の炉内部、煙道D内部、バイパス管32,33内部の少なくとも一箇所に戻す場合について説明したが、排ガス17の処理量が多いために脱硫排水28の量が増え、全量を戻せない場合には、脱硫排水28から有害物質を除去し、pHを調整した後、その一部を系外に排出してもよい。 In the example shown in FIG. 1, the entire amount of the desulfurization drainage 28 discharged from the desulfurization device 15 is supplied to the boiler 11, a path for supplying the fuel F, the furnace interior of the boiler 11, the flue D interior, and the bypass pipes 32 and 33. The case of returning to at least one place in the interior has been described, but when the amount of the exhaust gas 17 is large, the amount of the desulfurization waste water 28 increases, and when the entire amount cannot be returned, harmful substances are removed from the desulfurization waste water 28 and the pH is adjusted. After the adjustment, a part of it may be discharged out of the system.

 次に、実施例2に係る排ガス処理システムについて説明する。なお、上述した実施例1と同一の構成には同一の符号を付し、その説明を省略する。図2は、実施例2に係る排ガス処理システム10Bの概略構成図である。上述した実施例1では、脱硫装置15から排出される脱硫排水28の排水処理を行わずに、脱硫排水28をそのままボイラ11や煙道D内部の排ガス17中に噴霧する構成としたが、実施例2の排水処理システム10Bでは、排水ライン29の途中に固液分離装置35を設け、脱硫装置15からの脱硫排水28を固液分離装置35で固液分離し、その分離液(処理排水)をボイラ11に燃料Fを供給する経路、ボイラ11の炉内部、煙道D内部、バイパス管32,33内部に供給する構成とした点が、実施例1と異なっている。それ以外の構成は実施例1と同じである。 Next, an exhaust gas treatment system according to Example 2 will be described. In addition, the same code | symbol is attached | subjected to the structure same as Example 1 mentioned above, and the description is abbreviate | omitted. FIG. 2 is a schematic configuration diagram of an exhaust gas treatment system 10B according to the second embodiment. In the first embodiment described above, the desulfurization waste water 28 discharged from the desulfurization apparatus 15 is not subjected to waste water treatment, and the desulfurization waste water 28 is sprayed directly into the exhaust gas 17 inside the boiler 11 or the flue D. In the wastewater treatment system 10B of Example 2, a solid-liquid separation device 35 is provided in the middle of the drainage line 29, and the desulfurization wastewater 28 from the desulfurization device 15 is solid-liquid separated by the solid-liquid separation device 35, and the separated liquid (treated wastewater). Is different from the first embodiment in that the fuel F is supplied to the boiler 11 in the path for supplying the fuel F, the furnace 11 of the boiler 11, the flue D, and the bypass pipes 32 and 33. The other configuration is the same as that of the first embodiment.

 固液分離装置35は、脱硫排水28中の石膏を含む固体分と液体分とを分離するものである。固液分離装置35としては、例えばベルトフィルタ、遠心分離機、デカンタ型遠心沈降機等が用いられる。脱硫装置15から排出された脱硫排水28は、固液分離装置35により石膏37が分離される。その際、脱硫排水28中の塩化水銀は石膏37に吸着された状態で石膏37とともに液体と分離される。分離した石膏37は、システム外部(以下、「系外」という)に排出される。一方、分離液(処理排水)36は排水ライン29を介して排水タンク31に送られる。排水タンク31に貯留された分離液(処理排水)36は、排水供給管P0~P5を介してボイラ11に燃料Fを供給する経路、ボイラ11の炉内部、煙道D内部、バイパス管32,33内部に供給され、蒸発する。 The solid-liquid separation device 35 separates the solid component containing gypsum in the desulfurization waste water 28 from the liquid component. As the solid-liquid separator 35, for example, a belt filter, a centrifugal separator, a decanter type centrifugal sedimentator, or the like is used. The desulfurization waste water 28 discharged from the desulfurization device 15 is separated from the gypsum 37 by the solid-liquid separation device 35. At that time, mercury chloride in the desulfurization waste water 28 is separated from the liquid together with the gypsum 37 while being adsorbed on the gypsum 37. The separated gypsum 37 is discharged outside the system (hereinafter referred to as “outside system”). On the other hand, the separation liquid (treated wastewater) 36 is sent to the drainage tank 31 via the drainage line 29. The separated liquid (treated wastewater) 36 stored in the drainage tank 31 is supplied to the boiler 11 via drainage supply pipes P0 to P5, inside the furnace of the boiler 11, inside the flue D, bypass pipe 32, 33 is supplied inside and evaporates.

 このように、実施例2の排ガス処理システム10Bでは、脱硫装置15から排出される脱硫排水28から石膏37を分離し、その分離液36をボイラ11に燃料Fを供給する経路、ボイラ11の炉内部、煙道D内部、バイパス管32,33内部に供給する構成としている。上記のように構成したことで、実施例1の効果に加えて、煙道D内で排水が蒸発するのに伴い発生する乾燥粒子の量を実施例1と比べて低減させることができる。その結果、乾燥粒子の付着に起因する脱硝装置12での反応阻害や、脱硝装置12及びエアヒータ13の目詰まりを低減させることができるため、ノズルN1~N5の設置位置の自由度が向上する。また、脱硫排水28を固液分離することにより、石膏37とともに塩化水銀も分離・除去されるため、排水噴霧時に煙道D内部の排ガス17中の水銀濃度が増加するのを防止することができる。 As described above, in the exhaust gas treatment system 10B of the second embodiment, the gypsum 37 is separated from the desulfurization waste water 28 discharged from the desulfurization device 15, and the path for supplying the fuel F to the boiler 11 is supplied to the boiler 11. The inside is supplied to the inside of the flue D and the inside of the bypass pipes 32 and 33. By configuring as described above, in addition to the effect of the first embodiment, the amount of dry particles generated as the waste water evaporates in the flue D can be reduced as compared with the first embodiment. As a result, reaction inhibition in the denitration apparatus 12 due to adhesion of dry particles and clogging of the denitration apparatus 12 and the air heater 13 can be reduced, so that the degree of freedom of the installation positions of the nozzles N1 to N5 is improved. Further, by separating the desulfurized waste water 28 into solid and liquid, mercury chloride is separated and removed together with the gypsum 37, so that it is possible to prevent the mercury concentration in the flue gas 17 in the flue D from increasing when the waste water is sprayed. .

 次に、実施例3に係る排ガス処理システムについて説明する。なお、上述した実施例1,2と同一の構成には同一の符号を付し、その説明を省略する。図3は、実施例3に係る排ガス処理システム10Cの概略構成図である。上述した実施例2では、排水ライン29の途中に固液分離装置35を設け、脱硫装置15からの脱硫排水28を固液分離装置35で固液分離し、その分離液36をボイラ11に燃料Fを供給する経路、ボイラ11の炉内部、煙道D内部、バイパス管32,33内部に供給する構成としたが、実施例3の排ガス処理システム10Cでは、固液分離装置35の下流側にさらに排水処理装置38を設け、この排水処理装置38により分離液36中の有害物質や懸濁物等を除去した後、この処理排水39を排ガス17中に噴霧する構成とした点が、実施例2と異なっている。それ以外の構成は実施例2と同じである。 Next, an exhaust gas treatment system according to Example 3 will be described. In addition, the same code | symbol is attached | subjected to the structure same as Example 1, 2 mentioned above, and the description is abbreviate | omitted. FIG. 3 is a schematic configuration diagram of an exhaust gas treatment system 10C according to the third embodiment. In the second embodiment described above, the solid-liquid separation device 35 is provided in the middle of the drainage line 29, the desulfurization waste water 28 from the desulfurization device 15 is solid-liquid separated by the solid-liquid separation device 35, and the separated liquid 36 is supplied to the boiler 11 as fuel. Although it was set as the structure which supplies the path | route which supplies F, the furnace inside of the boiler 11, the flue D inside, and the bypass pipes 32 and 33 inside, in the waste gas treatment system 10C of Example 3, it is downstream of the solid-liquid separation apparatus 35. Further, the waste water treatment device 38 is provided, and after removing harmful substances and suspended matters in the separated liquid 36 by the waste water treatment device 38, the treated waste water 39 is sprayed into the exhaust gas 17 in the embodiment. Different from 2. The other configuration is the same as that of the second embodiment.

 排水処理装置38は、分離液36中に残存する水銀(石膏37に吸着しきれなかったもの)、ホウ素、セレン等の物質を除去する手段(以下では、「水銀除去手段」とよぶ)と、塩素イオン(Cl)、臭素イオン(Br),ヨウ素イオン(I),フッ素イオン(F)等のハロゲンイオンを除去する手段(以下では、「ハロゲンイオン除去手段」とよぶ)とを備えている。 The waste water treatment device 38 includes a means for removing substances remaining in the separation liquid 36 (those that could not be adsorbed on the gypsum 37), boron, selenium and the like (hereinafter referred to as "mercury removing means"), Means for removing halogen ions such as chlorine ions (Cl ), bromine ions (Br ), iodine ions (I ), fluorine ions (F ) (hereinafter referred to as “halogen ion removing means”); I have.

 水銀、ホウ素、セレン等の物質は水に溶けやすく、排ガス17中に噴霧した場合に揮発するため、集塵機14で除去することが困難である。これらの物質を除去する手段としては、硫化物系の凝集助剤添加による凝集により沈殿除去する手段、活性炭により吸着(浮遊床)除去する手段、キレート剤添加により沈殿除去する手段、晶析手段等が挙げられる。上記で例示される水銀除去手段により上記有害物質が固形化され、固形物は系外に排出される。 Substances such as mercury, boron and selenium are easily dissolved in water and volatilize when sprayed into the exhaust gas 17, and are therefore difficult to remove with the dust collector 14. Means for removing these substances include means for removing precipitates by flocculation by adding a sulfide-type flocculating aid, means for removing adsorbed (floating bed) by activated carbon, means for removing precipitates by adding a chelating agent, crystallization means, etc. Is mentioned. The harmful substance is solidified by the mercury removing means exemplified above, and the solid matter is discharged out of the system.

 また、上記のハロゲンイオンは、脱硫装置15の脱硫工程の際に水銀の石膏37への吸着を抑制する性質を持つため、脱硫排水28から除去するのが好ましい。上記のハロゲンイオンを除去する手段としては、逆浸透膜を用いた濃縮手段、イオン交換膜を用いた濃縮手段、電気透析法を用いた濃縮手段、蒸留、晶析等の手段が挙げられる。上記で例示されるハロゲンイオン除去手段によりハロゲンイオンが濃縮され、濃縮物は系外に排出される。 Further, the halogen ion is preferably removed from the desulfurization waste water 28 because it has the property of suppressing the adsorption of mercury to the gypsum 37 during the desulfurization process of the desulfurization apparatus 15. Examples of the means for removing the halogen ions include concentration means using a reverse osmosis membrane, concentration means using an ion exchange membrane, concentration means using an electrodialysis method, distillation, crystallization, and the like. Halogen ions are concentrated by the halogen ion removing means exemplified above, and the concentrate is discharged out of the system.

 脱硫装置15から排出された脱硫排水28は、まず、固液分離装置35により塩化水銀を吸着した石膏37が分離され、石膏37は系外に排出される。次いで、石膏37が除去された分離液36は、排水ライン29を介して排水処理装置38に送られ、水銀除去手段により分離液36中に残存する水銀、ホウ素、セレン等の有害物質が除去される。水銀を除去した後の処理排水はハロゲンイオン除去手段に送られ、ハロゲンイオンが除去される。ハロゲンイオンが除去された後の処理排水39は排水タンク31に送られる。排水タンク31に貯留された処理排水39は、排水供給管P0~P5を介して、ボイラ11に燃料Fを供給する経路、ボイラ11の炉内部、煙道D内部、バイパス管32,33内部に供給され、蒸発する。 The desulfurization waste water 28 discharged from the desulfurization device 15 is first separated from the gypsum 37 adsorbing mercury chloride by the solid-liquid separation device 35, and the gypsum 37 is discharged out of the system. Next, the separation liquid 36 from which the gypsum 37 has been removed is sent to a wastewater treatment device 38 via a drainage line 29, and harmful substances such as mercury, boron, and selenium remaining in the separation liquid 36 are removed by the mercury removing means. The The treated waste water after the mercury is removed is sent to a halogen ion removing means to remove halogen ions. The treated waste water 39 after the halogen ions are removed is sent to the drain tank 31. The treated wastewater 39 stored in the drainage tank 31 passes through the drainage supply pipes P0 to P5 to supply fuel F to the boiler 11, inside the furnace of the boiler 11, inside the flue D, and inside the bypass pipes 32 and 33. Supplied and evaporates.

 なお、排水処理装置38は、必ずしも上記の水銀除去手段とハロゲンイオン除去手段の両方を備える必要はなく、脱硫排水28の性状に応じて選択して設置する。例えば、脱硝装置12で水銀を酸化して塩化水銀に変換する処理を行う場合、Clは有用に用いられるため、ハロゲンイオン除去手段による処理を省略し、ハロゲンイオンを含有した状態の処理排水39を排ガス17中に噴霧してもよい。また、排水処理装置38の前段の固液分離装置35において水銀が十分に除去され、分離液36中の水銀含有量が極めて低いか、あるいは、水銀が含まれない場合には、水銀除去手段による処理を省略してもよい。 The waste water treatment device 38 is not necessarily provided with both the mercury removal means and the halogen ion removal means, and is selected and installed according to the properties of the desulfurization waste water 28. For example, when the denitration apparatus 12 performs a process of oxidizing mercury and converting it to mercury chloride, Cl 2 - is usefully used. Therefore, the treatment by the halogen ion removing means is omitted, and the treated waste water 39 containing halogen ions is used. May be sprayed into the exhaust gas 17. Further, when the mercury is sufficiently removed in the solid-liquid separation device 35 in the preceding stage of the waste water treatment device 38 and the mercury content in the separation liquid 36 is extremely low or does not contain mercury, the mercury removal means is used. Processing may be omitted.

 また、排水処理装置38での水銀除去処理とハロゲンイオン除去処理の順番は特に限定されない。すなわち、水銀除去処理の後にハロゲンイオン除去処理を行ってもよく、ハロゲンイオン除去処理の後に水銀除去処理を行ってもよい。 Also, the order of mercury removal treatment and halogen ion removal treatment in the waste water treatment device 38 is not particularly limited. That is, the halogen ion removal process may be performed after the mercury removal process, or the mercury removal process may be performed after the halogen ion removal process.

 以上のように、実施例3の排ガス処理システム10Cでは、脱硫装置15から排出される脱硫排水28から、まず、粗大物である石膏37を分離した後、水銀、ホウ素、セレン、ハロゲンイオン等の微細な物質を除去処理し、その処理排水39をボイラ11に燃料Fを供給する経路、ボイラ11の炉内部、煙道D内部、バイパス管32,33内部に供給する構成としている。上記のように構成したことで、実施例2と同様に、煙道D内で排水が蒸発するのに伴い発生する乾燥粒子の量を低減させることができるのに加えて、排水噴霧時に煙道D内部の排ガス17中の水銀濃度が増加するのを防止することができる。 As described above, in the exhaust gas treatment system 10C according to the third embodiment, the gypsum 37, which is a coarse material, is first separated from the desulfurization waste water 28 discharged from the desulfurization apparatus 15, and then mercury, boron, selenium, halogen ions, and the like are separated. A fine substance is removed and the treated waste water 39 is supplied to the boiler 11 through the path for supplying the fuel F, inside the furnace of the boiler 11, inside the flue D, and inside the bypass pipes 32 and 33. By being configured as described above, in addition to being able to reduce the amount of dry particles generated as the wastewater evaporates in the flue D, as in Example 2, in addition to the flue when spraying the wastewater It is possible to prevent the mercury concentration in the exhaust gas 17 inside D from increasing.

 次に、実施例4に係る排ガス処理システムについて説明する。なお、上述した実施例1~3と同一の構成には同一の符号を付し、その説明を省略する。図4は、実施例4に係る排ガス処理システム10Dの概略構成図である。上述した実施例3では、固液分離装置35の下流側に排水処理装置38を設けた構成としたが、実施例4では、排水処理装置38を固液分離装置35よりも上流側に設けた点が、実施例3と異なっている。それ以外の構成は実施例3と同じである。 Next, an exhaust gas treatment system according to Example 4 will be described. The same components as those in the first to third embodiments are denoted by the same reference numerals, and the description thereof is omitted. FIG. 4 is a schematic configuration diagram of an exhaust gas treatment system 10D according to the fourth embodiment. In the above-described third embodiment, the waste water treatment device 38 is provided on the downstream side of the solid-liquid separation device 35. However, in the fourth embodiment, the waste water treatment device 38 is provided on the upstream side of the solid-liquid separation device 35. This is different from the third embodiment. The other configuration is the same as that of the third embodiment.

 脱硫装置15から排出された脱硫排水28は、まず、排水処理装置38に送られ、脱硫排水28中に含まれる水銀、ホウ素、セレン等の微細な物質が、上述したように凝集、活性炭吸着、キレート、晶析等の手段によって固形化される。また、脱硫排水28中のCl、Br,I,F等のハロゲンイオンは、上述したように逆浸透膜、イオン交換膜、電気透析、蒸留等の濃縮手段により濃縮され、濃縮物が分離される。この後、水銀等の固形物を含んだ状態の処理排水41は、排水ライン29を介して固液分離装置35に送られ、塩化水銀を含んだ石膏37とともに、上記固形物が分離除去される。固液分離装置35で固形分と分離された分離液42は排水タンク31に送られる。排水タンク31に貯留された分離液(処理排水)42は、排水供給管P0~P5を介して、ボイラ11に燃料Fを供給する経路、ボイラ11の炉内部、煙道D内部、バイパス管32,33内部に供給され、蒸発する。 The desulfurization waste water 28 discharged from the desulfurization device 15 is first sent to the waste water treatment device 38, where fine substances such as mercury, boron and selenium contained in the desulfurization waste water 28 are aggregated, activated carbon adsorbed, It is solidified by means such as chelation and crystallization. Further, as described above, halogen ions such as Cl , Br , I , and F in the desulfurization waste water 28 are concentrated by a concentration means such as a reverse osmosis membrane, an ion exchange membrane, electrodialysis, distillation, and the like. Are separated. Thereafter, the treated wastewater 41 containing solids such as mercury is sent to the solid-liquid separator 35 via the drainage line 29, and the solids are separated and removed together with the gypsum 37 containing mercury chloride. . The separated liquid 42 separated from the solid content by the solid-liquid separator 35 is sent to the drainage tank 31. The separated liquid (treated wastewater) 42 stored in the drainage tank 31 is supplied through the drainage supply pipes P0 to P5 to the path for supplying the fuel F to the boiler 11, inside the furnace of the boiler 11, inside the flue D, and bypass pipe 32. , 33 is supplied to the inside and evaporated.

 このように、実施例4の排ガス処理システム10Dでは、脱硫装置15から排出される脱硫排水28から、まず、排水処理装置38で水銀、ホウ素、セレン、ハロゲンイオン等の微細な物質を固形化した後、固液分離装置35で石膏37とともに上記の固形物を分離し、その分離液42をボイラ11に燃料Fを供給する経路、ボイラ11の炉内部、煙道D内部、バイパス管32,33内部に供給する構成としている。上記のように構成したことで、実施例2と同様に、排水の蒸発に伴い発生する乾燥粒子の量を低減させることができるのに加えて、排水噴霧時に煙道D内部の排ガス17中の水銀濃度が増加するのを防止することができる。また、排水処理装置38で生成した固形物及び濃縮物は、後段の固液分離装置35で石膏37とともに分離・除去されるため、排水処理装置38での濾過工程を省略することができる。 Thus, in the exhaust gas treatment system 10D of Example 4, from the desulfurization waste water 28 discharged from the desulfurization device 15, first, a fine substance such as mercury, boron, selenium, or halogen ions was solidified by the waste water treatment device 38. Thereafter, the solid matter is separated together with the gypsum 37 by the solid-liquid separation device 35, and the separation liquid 42 is supplied to the boiler 11 with the fuel F, inside the furnace of the boiler 11, inside the flue D, and bypass pipes 32 and 33. It is configured to supply inside. By being configured as described above, in the same manner as in Example 2, in addition to being able to reduce the amount of dry particles generated along with the evaporation of the wastewater, in the exhaust gas 17 inside the flue D during drainage spraying It is possible to prevent the mercury concentration from increasing. Moreover, since the solid substance and concentrate produced | generated with the waste water treatment apparatus 38 are isolate | separated and removed with the gypsum 37 by the solid-liquid separation apparatus 35 of a latter stage, the filtration process in the waste water treatment apparatus 38 can be skipped.

 次に、実施例5に係る排ガス処理システムについて説明する。なお、上述した実施例1~4と同一の構成には同一の符号を付し、その説明を省略する。図5は、実施例5に係る排ガス処理システム10Eの概略構成図である。この実施例5では、上述した実施例4の構成に加えて、固液分離装置35の下流側にさらに第2の排水処理装置38Bを設けた構成としている。第2の排水処理装置38Bの構成は、固液分離装置35の上流側に設置される第1の排水処理装置38Aの構成と同様である。 Next, an exhaust gas treatment system according to Example 5 will be described. The same components as those in the first to fourth embodiments are denoted by the same reference numerals, and the description thereof is omitted. FIG. 5 is a schematic configuration diagram of an exhaust gas treatment system 10E according to the fifth embodiment. In the fifth embodiment, in addition to the configuration of the fourth embodiment described above, a second waste water treatment device 38B is further provided on the downstream side of the solid-liquid separation device 35. The configuration of the second wastewater treatment device 38B is the same as the configuration of the first wastewater treatment device 38A installed on the upstream side of the solid-liquid separation device 35.

 脱硫装置15から排出された脱硫排水28は、まず、第1の排水処理装置38Aに送られ、脱硫排水28中に含まれる水銀、ホウ素、セレン等の微細な物質が、上述した凝集、活性炭吸着、キレート、晶析等の手段を用いて固形化される。また、脱硫排水28中のCl、Br,I,F等のハロゲンイオンは、上述した逆浸透膜、イオン交換膜、電気透析、蒸留等の手段により濃縮される。水銀等の固形物及びハロゲンイオンの濃縮物を含んだ状態の処理排水41は、排水ライン29を介して固液分離装置35に送られ、塩化水銀を含んだ石膏37とともに、上記固形物及び濃縮物が分離・除去される。固液分離装置35で分離された分離液42は、第2の排水処理装置38Bに送られ、分離液42に残存する微量の水銀やハロゲンイオンが除去される。第2の排水処理装置38Bで処理された処理排水43は、排水タンク31に送られる。排水タンク31に貯留された処理排水43は、排水供給管P0~P5を介して、ボイラ11に燃料Fを供給する経路、ボイラ11の炉内部、煙道D内部、バイパス管32,33内部に供給され、蒸発する。 The desulfurization waste water 28 discharged from the desulfurization device 15 is first sent to the first waste water treatment device 38A, and fine substances such as mercury, boron and selenium contained in the desulfurization waste water 28 are aggregated and activated carbon adsorbed as described above. , Solidification using means such as chelation and crystallization. In addition, halogen ions such as Cl , Br , I and F in the desulfurization waste water 28 are concentrated by means such as the reverse osmosis membrane, ion exchange membrane, electrodialysis and distillation. The treated wastewater 41 containing a solid matter such as mercury and a halogen ion concentrate is sent to the solid-liquid separator 35 via the drainage line 29, and together with the gypsum 37 containing mercury chloride, the solid matter and the concentrated product. Things are separated and removed. The separation liquid 42 separated by the solid-liquid separation apparatus 35 is sent to the second waste water treatment apparatus 38B, and a trace amount of mercury and halogen ions remaining in the separation liquid 42 are removed. The treated wastewater 43 treated by the second wastewater treatment device 38B is sent to the drainage tank 31. The treated wastewater 43 stored in the drainage tank 31 passes through the drainage supply pipes P0 to P5 to supply fuel F to the boiler 11, inside the furnace of the boiler 11, inside the flue D, and inside the bypass pipes 32 and 33. Supplied and evaporates.

 このように、実施例5の排ガス処理システム10Eでは、脱硫装置15から排出される脱硫排水28から、まず、第1の排水処理装置38Aで水銀、ホウ素、セレン、ハロゲンイオン等の微細な物質を固形化した後、固液分離装置35で石膏37とともに上記の固形物を分離し、さらに、第2の排水処理装置38Bで分離液42に残存する微量の水銀やハロゲンイオンを除去した後の処理排水43をボイラ11に燃料Fを供給する経路、ボイラ11の炉内部、煙道D内部、バイパス管32,33内部に供給する構成としている。このように排水処理をより高精度に行うことで、排ガス17中に処理排水43を噴霧し蒸発させた場合に乾燥粒子がほとんど発生せず、また、排水噴霧時に煙道D内部の排ガス17中の水銀濃度が増加するのを確実に防止することができる。 As described above, in the exhaust gas treatment system 10E of the fifth embodiment, from the desulfurization waste water 28 discharged from the desulfurization device 15, first, fine substances such as mercury, boron, selenium, and halogen ions are obtained by the first waste water treatment device 38A. After solidification, the solid matter is separated together with the gypsum 37 by the solid-liquid separation device 35, and further, the treatment after removing traces of mercury and halogen ions remaining in the separation liquid 42 by the second waste water treatment device 38B. The drain 43 is supplied to the boiler 11 through the path for supplying the fuel F, the boiler 11 inside the furnace, the flue D, and the bypass pipes 32 and 33. By performing the wastewater treatment with higher accuracy in this way, almost no dry particles are generated when the treated wastewater 43 is sprayed and evaporated in the exhaust gas 17, and in the exhaust gas 17 inside the flue D when the waste water is sprayed. It is possible to reliably prevent an increase in mercury concentration.

 以上のように、本発明に係る排ガス処理システム及び排ガス処理方法は、脱硫装置から排出される脱硫排水の低減あるいは無排水化に有用である。 As described above, the exhaust gas treatment system and the exhaust gas treatment method according to the present invention are useful for reducing desulfurization drainage discharged from a desulfurization apparatus or eliminating drainage.

 10A,10B,10C,10D,10E 排ガス処理システム
 11 ボイラ
 12 脱硝装置
 13 エアヒータ
 14 集塵機
 15 脱硫装置
 16 排水噴霧装置
 17 排ガス
 20 石灰スラリー
 21 石灰スラリー供給装置
 22 塔底部
 23 ノズル
 24 塔頂部
 26 浄化ガス
 27 煙突
 28 脱硫排水
 29 排水ライン
 31 排水タンク
 32 バイパス管
 33 バイパス管
 35 固液分離装置
 36,42 分離液
 37 石膏
 38 排水処理装置
 39,41,43 処理排水
 P0,P1,P2,P3,P4,P5 排水供給管(排水供給手段)
 N1,N2,N3,N4,N5 ノズル
 F 燃料
10A, 10B, 10C, 10D, 10E Exhaust gas treatment system 11 Boiler 12 Denitration device 13 Air heater 14 Dust collector 15 Desulfurization device 16 Waste water spray device 17 Exhaust gas 20 Lime slurry 21 Lime slurry supply device 22 Tower bottom 23 Nozzle 24 Tower top 26 Purified gas 27 Chimney 28 Desulfurization drainage 29 Drainage line 31 Drainage tank 32 Bypass pipe 33 Bypass pipe 35 Solid-liquid separator 36, 42 Separation liquid 37 Gypsum 38 Wastewater treatment equipment 39, 41, 43 Treated wastewater P0, P1, P2, P3, P4, P5 Drainage supply pipe (drainage supply means)
N1, N2, N3, N4, N5 Nozzle F Fuel

Claims (18)

  1.  燃料を燃焼させるボイラと、
     前記ボイラからの排ガスの熱を回収するエアヒータと、
     熱回収後の排ガス中に含まれる硫黄酸化物を吸収液で除去する脱硫装置とを備えた排ガス処理システムにおいて、
     前記ボイラに燃料を供給する経路、前記ボイラの炉内部、前記ボイラと前記エアヒータとの間の煙道内部の少なくとも一箇所に、前記脱硫装置から排出される脱硫排水を供給する排水供給手段を備えることを特徴とする排ガス処理システム。
    A boiler that burns fuel;
    An air heater for recovering heat of exhaust gas from the boiler;
    In an exhaust gas treatment system equipped with a desulfurization device that removes sulfur oxides contained in exhaust gas after heat recovery with an absorption liquid,
    A drain supply means for supplying desulfurization drainage discharged from the desulfurization device is provided in at least one place in a path for supplying fuel to the boiler, in a furnace of the boiler, and in a flue between the boiler and the air heater. An exhaust gas treatment system characterized by that.
  2.  前記エアヒータの上流側に、前記ボイラからの排ガス中の窒素酸化物を除去する脱硝装置を備え、前記ボイラと前記脱硝装置との間、又は、前記脱硝装置と前記エアヒータとの間の少なくとも一方に前記排水供給手段を設けたことを特徴とする請求項1に記載の排ガス処理システム。 A denitration device that removes nitrogen oxides in the exhaust gas from the boiler is provided on the upstream side of the air heater, and at least one between the boiler and the denitration device or between the denitration device and the air heater. The exhaust gas treatment system according to claim 1, wherein the waste water supply means is provided.
  3.  前記脱硝装置と並列な位置、又は、前記エアヒータと並列な位置の少なくとも一方にバイパス管を設け、前記バイパス管に前記排水供給手段を設けたことを特徴とする請求項2に記載の排ガス処理システム。 The exhaust gas treatment system according to claim 2, wherein a bypass pipe is provided at at least one of a position parallel to the denitration device or a position parallel to the air heater, and the waste water supply means is provided to the bypass pipe. .
  4.  燃料を燃焼させるボイラと、
     前記ボイラからの排ガスの熱を回収するエアヒータと、
     熱回収後の排ガス中に含まれる硫黄酸化物を吸収液で除去する脱硫装置とを備えた排ガス処理システムにおいて、
     前記脱硫装置から排出される脱硫排水から有害物質を除去処理する排水処理手段と、
     前記ボイラに燃料を供給する経路、前記ボイラの炉内部、前記ボイラと前記エアヒータとの間の煙道内部の少なくとも一箇所に設置され前記排水処理手段で処理された処理排水を噴霧する排水供給手段と、
     を備えることを特徴とする排ガス処理システム。
    A boiler that burns fuel;
    An air heater for recovering heat of exhaust gas from the boiler;
    In an exhaust gas treatment system equipped with a desulfurization device that removes sulfur oxides contained in exhaust gas after heat recovery with an absorption liquid,
    Waste water treatment means for removing harmful substances from the desulfurization waste water discharged from the desulfurization apparatus,
    Waste water supply means for spraying the treated waste water which is installed in at least one place inside the furnace, the flue between the boiler and the air heater, and which has been treated by the waste water treatment means. When,
    An exhaust gas treatment system comprising:
  5.  前記エアヒータの上流側に、前記ボイラからの排ガス中の窒素酸化物を除去する脱硝装置を備え、前記ボイラと前記脱硝装置との間、又は、前記脱硝装置と前記エアヒータとの間の少なくとも一方に前記排水供給手段を設けたことを特徴とする請求項4に記載の排ガス処理システム。 A denitration device that removes nitrogen oxides in the exhaust gas from the boiler is provided on the upstream side of the air heater, and at least one between the boiler and the denitration device or between the denitration device and the air heater. The exhaust gas treatment system according to claim 4, wherein the waste water supply means is provided.
  6.  前記脱硝装置と並列な位置、又は、前記エアヒータと並列な位置の少なくとも一方にバイパス管を設け、前記バイパス管に前記排水供給手段を設けたことを特徴とする請求項5に記載の排ガス処理システム。 6. The exhaust gas treatment system according to claim 5, wherein a bypass pipe is provided in at least one of a position parallel to the denitration device or a position parallel to the air heater, and the waste water supply means is provided in the bypass pipe. .
  7.  前記排水処理手段は、前記脱硫装置から排出される脱硫排水中の固体分と液体分とを分離する固液分離装置を備えることを特徴とする請求項4に記載の排ガス処理システム。 The exhaust gas treatment system according to claim 4, wherein the waste water treatment means includes a solid-liquid separation device that separates a solid content and a liquid content in the desulfurization waste water discharged from the desulfurization device.
  8.  前記排水処理手段は、前記脱硫装置から排出される脱硫排水に含まれる水銀を除去する水銀除去装置を備えることを特徴とする請求項4に記載の排ガス処理システム。 The exhaust gas treatment system according to claim 4, wherein the waste water treatment means includes a mercury removal device for removing mercury contained in the desulfurization waste water discharged from the desulfurization device.
  9.  前記排水処理手段は、前記脱硫装置から排出される脱硫排水中に含まれるハロゲンイオンを除去するハロゲンイオン除去装置を備えることを特徴とする請求項4に記載の排ガス処理システム。 The exhaust gas treatment system according to claim 4, wherein the waste water treatment means includes a halogen ion removal device that removes halogen ions contained in the desulfurization waste water discharged from the desulfurization device.
  10.  燃料を燃焼させるボイラからの排ガスの熱をエアヒータにより回収した後、
     脱硫装置において、熱回収後の排ガス中に含まれる硫黄酸化物を吸収液で除去する排ガス処理方法において、
     前記ボイラに燃料を供給する経路、前記ボイラの炉内部、前記ボイラと前記エアヒータとの間の煙道内部の少なくとも一箇所に、前記脱硫装置から排出される脱硫排水を供給することを特徴とする排ガス処理方法。
    After recovering the heat of the exhaust gas from the boiler that burns the fuel with an air heater,
    In the desulfurization apparatus, in the exhaust gas treatment method for removing sulfur oxides contained in the exhaust gas after heat recovery with an absorption liquid,
    The desulfurization drainage discharged from the desulfurization device is supplied to at least one place in the path for supplying fuel to the boiler, the furnace interior of the boiler, and the flue between the boiler and the air heater. Exhaust gas treatment method.
  11.  前記エアヒータの上流側に、前記ボイラからの排ガス中の窒素酸化物を除去する脱硝装置を配置し、前記ボイラと前記脱硝装置との間、又は、前記脱硝装置と前記エアヒータとの間の少なくとも一方に前記脱硫排水を供給することを特徴とする請求項10に記載の排ガス処理方法。 A denitration device that removes nitrogen oxides in the exhaust gas from the boiler is disposed upstream of the air heater, and at least one of the space between the boiler and the denitration device, or between the denitration device and the air heater. The exhaust gas treatment method according to claim 10, wherein the desulfurization waste water is supplied to the exhaust gas.
  12.  前記脱硝装置と並列な位置、又は、前記エアヒータと並列な位置の少なくとも一方にバイパス管を設け、前記バイパス管の内部に前記脱硫排水を供給することを特徴とする請求項11に記載の排ガス処理方法。 The exhaust gas treatment according to claim 11, wherein a bypass pipe is provided in at least one of a position parallel to the denitration device or a position parallel to the air heater, and the desulfurization drainage is supplied into the bypass pipe. Method.
  13.  燃料を燃焼させるボイラからの排ガスの熱をエアヒータにより回収した後、
     脱硫装置において、熱回収後の排ガス中に含まれる硫黄酸化物を吸収液で除去する排ガス処理方法において、
     前記脱硫装置から排出される脱硫排水から有害物質を除去する排水処理を行った後、前記ボイラに燃料を供給する経路、前記ボイラの炉内部、前記ボイラと前記エアヒータとの間の煙道内部の少なくとも一箇所に、前記排水処理で処理した処理排水を供給することを特徴とする排ガス処理方法。
    After recovering the heat of the exhaust gas from the boiler that burns the fuel with an air heater,
    In the desulfurization apparatus, in the exhaust gas treatment method for removing sulfur oxides contained in the exhaust gas after heat recovery with an absorption liquid,
    After performing wastewater treatment to remove harmful substances from the desulfurization wastewater discharged from the desulfurization device, a path for supplying fuel to the boiler, inside the furnace of the boiler, and inside the flue between the boiler and the air heater An exhaust gas treatment method characterized by supplying the treated wastewater treated by the wastewater treatment to at least one place.
  14.  前記エアヒータの上流側に、前記ボイラからの排ガス中の窒素酸化物を除去する脱硝装置を配置し、前記ボイラと前記脱硝装置との間、又は、前記脱硝装置と前記エアヒータとの間の少なくとも一方に前記処理排水を供給することを特徴とする請求項13に記載の排ガス処理方法。 A denitration device that removes nitrogen oxides in the exhaust gas from the boiler is disposed upstream of the air heater, and at least one of the space between the boiler and the denitration device, or between the denitration device and the air heater. The exhaust gas treatment method according to claim 13, wherein the treated waste water is supplied to the exhaust gas.
  15.  前記脱硝装置と並列な位置、又は、前記エアヒータと並列な位置の少なくとも一方にバイパス管を設け、前記バイパス管の内部に前記処理排水を供給することを特徴とする請求項14に記載の排ガス処理方法。 The exhaust gas treatment according to claim 14, wherein a bypass pipe is provided in at least one of a position parallel to the denitration device or a position parallel to the air heater, and the treated waste water is supplied into the bypass pipe. Method.
  16.  前記排水処理は、前記脱硫装置から排出される脱硫排水中の固体分と液体分とを分離する固液分離処理を含むことを特徴とする請求項13に記載の排ガス処理方法。 The exhaust gas treatment method according to claim 13, wherein the waste water treatment includes a solid-liquid separation treatment for separating a solid content and a liquid content in the desulfurization waste water discharged from the desulfurization apparatus.
  17.  前記排水処理は、前記脱硫装置から排出される脱硫排水に含まれる水銀を除去する水銀除去処理を含むことを特徴とする請求項13に記載の排ガス処理方法。 The exhaust gas treatment method according to claim 13, wherein the waste water treatment includes a mercury removal treatment for removing mercury contained in the desulfurization waste water discharged from the desulfurization apparatus.
  18.  前記排水処理は、前記脱硫装置から排出される脱硫排水中に含まれるハロゲンイオンを除去するハロゲンイオン除去処理を含むことを特徴とする請求項13に記載の排ガス処理方法。 The exhaust gas treatment method according to claim 13, wherein the waste water treatment includes a halogen ion removal treatment for removing halogen ions contained in the desulfurization waste water discharged from the desulfurization apparatus.
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